Apparatus for combining vapors



Y Dec.

3 Sheets-Sheet 1 Dec 29, 1970 J.|..1c:HTENsT|-:|N 3,551,298

APPARATUSL FOR COMBINING vAPoRs Filed nec. 11 1967 s sheets-sheet 2 INVISNIUR.

D- 29 1970 J. LlcHTENsTElN 3,551,298

APPARATUS FOR COMINING VAPORE;

Filed Dec. 11. 1967 s sneets-sheet s vLvVEAf/UR. H @EPH lfoqre/ysre/N E L` BY 1 www@ United States Patent 3,551,298 APPARATUS FOR COMBINING VAPORS Joseph Lichtenstein, Bayside, N.Y., assigner to Saline Water` Conversion Corporation, Oradell, NJ., a corporation of New York Filed Dec. 11, 1967, Ser. No. 689,655 lut. Cl. Bld 3/06; C02b 1/06 U.S. Cl. 202-173 6 Claims ABSTRACT 0F THE DISCLOSURE An evaporative recovery system employing flash evaporation in finite multiple steps approaching thermodynamic reversibility. The respective vapor streams of each step are combined in a remote nozzle system which utilizes the respective pressure differentials between the respective steps to bring all the vapor streams to a common flow velocity in a common stream. The kinetic energy of the common stream thus obtained is recompressed in a diffusor into corresponding pressure for condensation.

This invention relates to the recovery of selected liquids from solution and more particularly it concerns improvements to evaporative type liquid recovery systems.

The present invention is especially useful in evaporative systems designed to recover salt free fresh water from sea lwater. Basically, vaporative recovery systems provide means for evaporating a portion of the incoming sea Water, separating the vapors so formed and thereafter condensing these vapors to fresh -water in liquid form.

Of the methods available to accomplish the above operation, the flash type of evaporation to-date is the predominant method employed. Such flash type evaporation is carried out by subjecting sea water at near saturation conditions to a reduced pressure. This produces evaporation of a portion of the water; and the heat of evaporation, which is obtained directly from the remaining unevaporated liquid, does not have to pass through vessel Walls or other heat transfer barriers.

The realization of a flash, that is the cooling by evaporation of a liquid from an initial temperature to a lower end temperature can be carried out in a variety of ways, starting from the thermodynamically ideal process of complete reversibility to the more usual process of complete irreversibility. The reversible process requires that evaporation take place in an infinitely large number of small temperature steps, thus ensuring, by the resulting minute vapor release velocities, the production of a pure vapor. Even more significant, however, is the fact that in this process each incremental `Vapor element produced is at the pressure corresponding to its temperature and thus possesses an enthalpy potential in relation to the enthalpy at the end of the flash. By expansion, each yvapor element can, therefore, be given a kinetic energy corresponding to its enthalpy potential.

It 'will be appreciated however, that the enthalpy potential for each successive incremental vapor element is different. Thus the first element, which vaporizes at the inlet temperature of the liquid, will possess the full enthalpy potential corresponding to the total flash, whereas the last element, vaporizing at the end temperature of the flash, will have none. Theoretical calculations show that the total vapor mass may be assumed to be conccntrated at the middle temperature of the flash. Thus by expansion a kinetic energy is obtained which corresponds to the enthalpy potential from the middle to end of the flash.

The kinetic energy of the total mass of vapor can be reconverted into pressure in an ideal frictionless diffusor, and it will by such compression reach the middle temperature of the flash. In order for such compression to be effective, the vapor phase in the diffusor must be entirely separated from the liquid phase of evaporation. Otherwise the heat of recompression will result in the condensation of vapor on the colder liquid phase. Thus, for example, an ideal flash process proceeding from 100 to would by recompression result in a vapor temperature of at which temperature it could be coudensed.

The irreversible process of flashing employed in prior art flash distillation is characterized by the fact that Water at saturation pressure corresponding to its initial temperature is suddenly entered into a space of reduced pressure corresponding to the end temperature of the flash. The resulting violent flash produces the total vapor mass instantaneously at a saturation temperature corresponding to the end temperature of the flash. No enthalpy potential is available for recompression. The violence of the flash results in tearing off particles from the evaporating liquid, and creates a mist which is carried along by the produced vapors into the condenser, contaminating the final condensate with undesired salinity. To protect the product from too much contamination, demisters must be employed Iwhich offer resistance to the vapor flow and correspondingly further reduce its temperature. Thus, for example, such a flash proceeding from to 90, and with a demister loss of say 2, would produce vapor in the condenser of a temperature of 88 as against 95 in the ideal process.

The above temperature difference if totally assigned to the terminal temperature difference of the condenser; the condenser surface required in an ideal flash process would be only a fraction of that which is required for conventional flash systems. On the other hand, if this temperature difference is assigned to the rise in condenser coolant temperature, a substantial reduction in heat required to maintain the flash cycle would result.

The present invention makes possible a flash type evaporation process which very closely approaches the ideal reversible process, and thereby overcomes the inefficiencies inherent in the flash systems previously utilized to-date. With the present invention, the energy contained within the flash is preserved with a high degree of efficiency so that the cost of producing fresh water by desalination is significantly reduced.

The actual realization of a flash process approaching that of the ideal reversible process is accomplished according to the present invention through the following steps.

First, the infinite number of temperature steps required by the ideal process is replaced by a finite number of steps. The total temperature differential of the flash is subdivided by a relatively small number `of temperature steps.

Next, the vapor phase is physically separated from the liquid phase. This separation is accomplished in the present invention in a novel manner, that is, by poducing two entirely separate streams and connecting both by relatively large channels in which vapors produced in the first stream can flow at low velocity to join the second stream.

In the first stream brine flows through a series of cells, the number of which corresponds to the subdivision of temperature steps of the flash. The cells are separated from each other by resistance elements, producing required pressure differentials between successive cells and establishing in each cell the pressure required for evaporation to produce the vapors of the desired temperatures.

In the second stream the vapors produced in the evaporation cells, and flowing through the interconnecting channels are combined in the following manner.

Patented Dec. 29, 1970 First, the incoming brine is forced through the first resistance element and enters the first cell at a pressure fractionally lower than its saturation pressure. A certain amount of vapor is thus produced in the first cell. This vapor flows through its interconnecting channel to the first nozzle, which straddles the first and second cells. This vapor in passing through the nozzle is subjected to the pressure differential existing between these two cells. The vapor expands and obtains a kinetic energy corresponding to the existing pressure differential.

The vapor produced in the second cell is brought into contact, through its interconnecting channel, with the discharge of the first nozzle. By momentum exchange the two vapor streams mix and obtain a common but lower velocity than the discharge velocity of the first nozzle. The resulting mixture then expands through the second nozz-le and obtains an increase in kinetic energy corresponding to the pressure differential existing between second and third cells. This process continues to the last nozzle, whose discharge is in contact, through its interconnecting channel, with the last cell. The vapor produced in the last cell mixes with the discharge of the last nozzle. The total vapor mass at this point is at maximum velocity. It then enters the diffusor.

In the diffusor, the kinetic energy of the total vapor mass is converted into pressure energy, so that at its discharge the vapor mass has reached its maximum pressure obtainable in the system and consequently can be condensed at its maximum temperature.

It will be appreciated that by the present invention,

the vapors which are formed at different pressure and temperature in the various steps of a multistep evaporation system are efficiently condensed in a common condenser. This aspect of the invention involves the equalization of the thermodynamic energy or enthalpy of the vapors in the various stages, so that they may be intermingled in a common condenser region without violent effects. The equalization of enthalpy of the vapors is achieved with minimal energy loss by passing the high enthalpy vapors (those at higher temperatures and pressure) through nozzles which convert a portion of their thermodynamic energy or enthalpy to kinetic energy of flow. The resulting flow is directed in such a manner as to sweep along the vapors from the next lower stage. The combined vapors are thus eventually brought to a common flow and together may be further reduced in enthalpy and increased in flow to a next lower stage. Eventually, all the vapors come to a common velocity, temperature and pressure. The velocity energy is thereafter reconverted into increased temperature and pressure (i.e. increased thermodynamic energy or enthalpy) in a diffusor for more effective condensation in the condenser region.

There has thus been outlined rather broadly the more important features of the invention in order that the detailed description thereof that follows may be better understood, and in order that the present contribution to the art may be better appreciated. There are, of course, additional features of the invention that will be described hereinafter and which will form the subject of the claims appended hereto. Those skilled in the art will appreciate that the conception upon which this disclosure is based may readily be utilized as a basis for the designing of other structures for carrying out the several purposes of the invention. It is important, therefore, that the claims be regarded as including such equivalent constructions as do not depart from the spirit andv scope of the invention.

A spceific embodiment of the invention has been chosen for purposes of illustration and description, and is shown in the accompanying drawings forming a part of the specification, wherein:

FIG. l is a perspective view, partially in section, of an evaporation and vapor separation stage of a system embodying the present invention;

FIG. 2 is a section view taken along line 2-2 of FIG. l; and

FIG. 3 is a view similar to FIG. 1 illustrating multiple and staging arrangements utilized in that system.

As shown in FIGS. 1 and 2, the evaporation and vapor separation system is enclosed Within an outer shell which includes stepped upstanding side walls 12 and 14, a vertical rear wall 16 and a front wall (not shown). A horizontal cover plate 18 extends over the central portion of the interior of the shell 10 near the top thereof. This cover plate has a pair of downwardly depending sides 20 which cooperate with the corresponding shell side walls 12 and 14 to define a pair of first step brine reservoirs 22a. The bottoms of these brine reservoirs are formed by a pair of first step orifice plates 24a which lie horizontally across the spaces between the sides 20 of the cover plate 18 and the corresponding side walls 12 and 14 of the outer shell 10.

A pair of inlet pipes 26 are provided to supply heated brine to be desalinized from an external source (not shown), to the first step brine reservoirs 22a.

The first step orifice plates 24a are provided with orifices 28 through which the brine may flow. Immediately under each of the plates 24a there is maintained a mass of packing material 30 which is held in place by a wire mesh or screen 32. This packing material is porous and permits liquid and vapors to flow downwardly through it. It serves, however, to prevent violet foaming effects which tend to occur as the brine passes through the orifices 28.

lImmediately below each mass of packing material 30 there is provided a first step vapor recovery zone 34a; and below that is provided a second step brine reservoir 2212. These regions are bound laterally by the side Walls 12 and 14 of the outer shell 10 and by side walls 36a of a first step nozzle plate 38a. The nozzle plate 38a is of the same general configuration as the cover plate 18 except that the nozzle plate 38a is formed with a first step nozzle 40a along its center. The nozzle plate 38a is partially nested Within the cover plate 18 and cooperates with the cover plate 18 to form first step vapor separating conduits 42a which extend from the first step vapor recovery zones 34a to the centrally located first step nozzle 40a.

A pair of second step orifice plates 2417, similar to the first step orifice plates 24a, extend respectively between the two outer shell walls 12 and 14 and the side Walls 36 of the first step nozzle plate 38a. These second step orifice plates, which define the bottom of the second step brine reservoir 22b are also provided with orifices 28- through which brine may ow. Also, there is maintained a mass of packing material 30 under each of these second step orifice plates 24b.

Below the packing material 30 under each second step orifice plate 24h, there is formed a second step vapor recovery zone 34h; and below that, a third step brine reservoir 22e.

A second step nozzle plate 38b, having a central second step nozzle opening 4Gb, and side walls 3617 is arranged just under and in partially nested relationship with the first step nozzle plate 38a. The side walls 3617 of the second step nozzle plate 38b cooperate with the side walls 36a of the first step nozzle plate 38a to form second step vapor separating conduits 4279 which extend from the second step vapor recovery zones 34b to the centrally located second step nozzle 40b.

In the same manner, there are provided third, fourth and fifth step brine reservoirs 22e-e, orifice plates 24e-e, vapor recovery zones 34e-e, nozzles plates 38e-e and vapor separating conduits 42e-e.

The third and fourth step nozzle plates 38C and d are provided with associated central nozzle openings 40e and a'. The fifth step nozzle plate 38e, however, is provided with a central diffusor opening which opens into a downwardly extending outwardly fiaring difiusor 52.

Below the fifth step vapor recovery zones 34e there are provided brine recovery channels 54 and 56 which collect unevaporated brine from the fifth veporization step. The recovery channels `54 direct this brine to chan- 'nels 56 which in turn directs the brine to a successive vaporization stage or, in the event there are none, to a discharge conduit (not shown).

The vapor which passes down through the central diffusor opening 50i, is ycaused by the diffusor 52 to undergo an energy conversion whereby its high kinetic energy of fiow is converted to thermodynamic energy of pressure and temperature.

It will be appreciated that the various orifice plates 24 and the vapor recovery zones 34 constitute a series of evaporator cells which define a first :fiow path down through which brine may flow. Similarly the nozzle plates 38 constitute a series of vapor mixing cells interconnected by the nozzles 40` to define a second separate fiow path down through which vapors may fioW. The evaporator cells and mixing chambers are interconnected by the vapor separating conduits 42.

In operation of the above described system, brine which has been heated to its saturation temperature is supplied via the inlet conduits tothe first stage liquid reservoirs 22a. The heated brine then passes through the orifice 28 in the first stage orifice plates 24a and fiows down through the mass of packing material 30 and the first step vapor recovery zones 34a into the second step liquid reservoirs 22h.

The pressure within the first step vapor recovery zones 34a is maintained differentially below that in the first step liquid reservoirs so that as the brine flows through the orifices 28 a portion of it evaporates. The heat required for this evaporation is taken from the unevaporated portion of the brine; and as a consequence it becomes reduced in temperature as it passes into the second step liquid reservoirs 22h.

The liquid brine in the second step reservoirs 22h fiows down through the orifices 42'8 in the second step orifice plates 24h andk passes down through the packing material 30, and the second step vapor recovery zones 34h into the third step liquid reservoirs 22e. The pressure in the second step vapor recovery zones 34b in turn is maintained differentially below that in the second step liquid reservoirs 22b. Thus, further evaporation and a further temperature depression occurs in these zones. This evaporation process continues down through each of the steps in the system.

The vapors in each vapor recovery zone 34a-f pass upwardly through their respective vapor separating conduits `12a-f. These conduits, it will be noted, are large relative to their associated vapor recovery zone. As a result, the lineal velocity of the vapors through the vapors separating conduits 42a-f is quite low. This permits liquid droplets associated with the vapors to fall back down to the liquid reservoirs 2'2. Thus, the vapors are substantially separated from the evaporated liquid by the time they reach the nozzle openings 40u-e.

The nozzle openings 40u-e, it will be noted, communicate between vapor separating conduits of successively lower pressure. Accordingly, the vapors pass through the nozzle openings in the direction of lower pressure. The nozzle openings are specially shaped to convert the thermodynamic energy of the vapors in a higher step to kinetic energy of high velocity flow in a lower step. Thus, the vapors are allowed to expand during their passage through the nozzle openings; and this expansion is controlled by the nozzle configuration so that it is converted to a high velocity flow in a downward direction.

The rapid rush of vapors down through the center of each of the vapor separating conduits 42af produces an aspirating effect whereby the slowly moving vapors in each conduit are drawn in with the rapidly moving vapors and are caused to move down through the next successive nozzle in the system. Thus, more and more vapors are caused to fiow down through lower and lower steps and in doing so they attain higher and higher velocities.

The mixing of the vapors in each step takes place by design in accordance with the principle of conservation of momentum which not only insures that the mixing process proceeds with minimum energy losses, but equally insures that after mixing, pressure and temperature are also equalized.

The mixing process, it will be appreciated, is associated with a certain amount of energy losses. However, theory shows that the loss is a mini-mum when the mixing proceeds with conservation of momentum. Also, the loss is smaller when the mass of the stream being taken along is small with respect to the mass of the stream taking it and when the inlet velocity of the latter is large.

The largest ratio of these vapor masses occurs at the discharge of the first nozzle. There the two masses are the same. The ratio then decreases towards the last nozzle. Since these losses affect the overall efficiency of the utilization of the flash energy and in order to maximize this efficiency, it may become desirable to increase the vapor velocities entering the respective nozzle system above that existing in the interconnecting channels. This requires an expansion of the vapor from the area of the interconnecting channel to a smaller entering area into the nozzle system. Such an expansion can only take place at the expense of pressure, that is at a reduction of the vapor temperatures in the nozzle system.

When the vapors reach the diffuser opening 50, they are directed thereby into the diffuser 52 where, because of gradually increasing fiow areas, vapor velocities are reduced and its kintic energy is changed into pressure energy and correspondingly increased temperature. Accordingly, the vapors are more easily condensed by a common fixed sized condenser supplied by a fixed quantity of cooling water at a fixed temperature.

FIG. 3 shows an arrangement for multistaging the multistep evaporation unit shown in FIGS. 1 and 2. In the multistaging arrangement there are provided several multistep evaporators 60, 62, 64 and 66. The evaporators 60 and 64 are arranged in vertical alignment and are paralleled by the evaporators 62 and 66, also arranged in vertical alignment. The upper evaporators 60` and 62 are separated from the lower evaporators 64 and 66 by common condenser regions 70 in which are located banks of condenser tubes 72. The vapors pass down through diffusors 50 and are converted thereby to higher pressures and tempeartures, and admitted at low velocity into the condenser regions 70. These vapors then contact the condenser tubes 72 and are converted thereby to liquid form. The resulting liquid condensate drips into a fresh water reservoir 74 and is then collected via various conduit means (not shown).

The unevaporated liquid from the upper evaporators 60 and 62 passes directly from their brine recovery channels 54 and 56, down to the brine inlet pipes 26 at the top of the lower evaporators 64 and 66. The evaporation process is then repeated at lower conditions of pressure and temperature.

It will be appreciated that the idea dividing the downwardly flowing fluids into two separate streams as above described permits very great fiexibility in design. Thus, the nozzle sizes can be established to optimize the mixing process without adversely affecting the evaporation process. Conversely, the temperature gradient down through the evaporator cells can be set to obtain maximum efiicieni cy Without adversely affecting the nozzle function.

The number of stages may be increased as desired. The multistep arrangement, however, permits the use of a fewer number of stages for a given overall temperature differential since it permits a single stage to handle flash type evaporation over a greater temperature range without incurring the turbulence problems associated with conventional fiash evaporation.

By reducing the number of stages in a system, the present invention reduces the number of separate condensers and associated equipment required. Also, by virtue of the diffusor arrangement used in the present invention, the effectiveness of the condenser itself is increased since it is enabled to extract more heat energy out of the vapors to be condensed.

It will be appreciated that in the arrangement of the present invention a common condenser unit may be used temperature, said chambers being arranged in series according to 'an order of successively decreasing interior pressures and temperatures, expansion nozzle means interconnecting adjacent chambers in said series whereby vapors of higher pressure and temperature will expand to condense the vapors which are formed in several steps and pass at high velocity from one chamber into the next at various conditions of pressure and temperature. This and combine with the vapors in said next chamber and is achieved by reducing the pressure and temperature of the combined vapors expand and pass at high velocity the vapors in the higher steps and by causing such reducfrom said next chamber into another chamber and so on, tion to take place via a nozzle so that the energy is not 10 and condenser means connected to the last chamber in wasted but is preserved in the form of high velocity flow. the series to receive and condense the combined vapors, It will be appreciated that the system of the present ineach of said expansion nozzle means being in mutual vention achieves its advantageous results, in part, by alignment and increased in size from nozzle to nozzle. causing expansion to occur separate from and at a location 3. Apparatus according to claim 2 further including remote from actual vaporization. In prior systems the vadiffuser means arranged in the path of -vapor ow into pors expanded in one step as they were formed, and this said condenser means to convert the vapor flow velocity expansion, because it took place adjacent to the liquid from to pressure in said condenser. which the vapor came, inevitably caused a tearing away 4. Apparatus for recovering selected vapors from a of liquid particles which contaminated the vapors upon solution, said apparatus comprising a plurality of evaporasubsequent condensation. In the present invention the tor cells, means dening a rst flow path constituted by vaporization takes place through the nozzle openings resaid evaporator cells arranged in series to permit liquid mote from the liquid brine. to be evaporated to pass serially therethrough, means for An experimental unit congured in accordance with maintaining said cells at successively decreasing presthe drawings herein, was built and operated in order to sures and temperatures whereby vapors are formed `from demonstrate the feasibility of the present invention. This said liquid at different pressures and temperatures in said unit was designed to accommodate a 6 gal./minute brine cells, means dening a plurality of vapor chambers each flow and the flash evaporate this brine from 105 down communicating with an associated one of said evaporator to 90 F. in five stages. By virtue of the dilfusor arrangecells to receive the vapors produced therein, expansion ment the temperature of the vapors was raised to 94 F. nozzle means interconnecting adjacent ones of said vapor for entry into the condenser region. chambers to permit vapors of higher pressure and tem- The unit tested had an overall height of about 17 inches, perature to expand and pass at high velocity from one a Width of about 101/2 inches and a depth of about 4 chamber into the next and combine with the vapors in the inches. The various other dimensions and operating connext chamber and further to permit the combined vapors ditions for the different steps are given in Table I. from said next chamber to expand and Pass at high V610- TABLE I Vapor tiow' Vapor I Pressure, Temp rate, 1b.] velocity, Dimension Dimension Dimension Dimension Dimension step p.s.i.a. seexlo-s msec. A, in. B, in. in. D, in. E, in.

Dimensions F and G were 10 inches and 2.5 inches, city from said next chamber into another and so on, and respectively. The dimensions may, of course, be adjusted condenser means connected to the chamber of lowest in accordance with the ow rate, the ash temperature pressure and temperature to receive and condense all of range and the number of steps employed. the combined vapors, each of said expansion nozzle means Having thus described my invention with particular being in mutual alignment and increased in size from reference to the preferred form thereof, it will be obvious nozzle to nozzle. to those skilled in the art to which the invention pertains, 5. In a multistage evaporative recovery system the after understanding my invention, that various changes combination of means defining two separate flow paths, and modifications may be made therein without departing one of said flow paths being constituted by a series of from the spirit and scope of my invention, as defined by evaporator cells arranged to be maintained at successivethe claims 'appended thereto. ly lower pressures land interconnected to permit liquid What is claimed as new and desired to be secured by to be evaporated to ow serially therethrough, said Letters Patent is: evaporator cells being arranged in vertical alignment, a 1. Apparatus for combining vapors comprising a plucommon condenser below said evaporator cells, means rality of chambers for containing vapors, means assodefining a common vapor recovery flow passage conciated with said chambers for maintaining the vapors in stituted by a series of vapor mixing chambers comsaid chambers at different conditions of pressure and municating with the evaporators and disposed centrally temperature, said chambers being arranged in series acand Ibetween the evaporators with expansion nozzle means cording to an order of successively descending interior of progressively increasing diameter from the upper pressure and temperatures, and expansion nozzle means to the lower evaporators for passing the vapor downinterconnecting Iadjacent chambers in said series whereby wardly in the common flow passage to the condenser. vapors of higher pressure and temperature will expand 6. Apparatus for combing vapors comprising 'a plurality and pass at high velocity from one chamber into the next of chambers for containing vapors, means associated with and combine with the vapors in said next chamber and said chambers for maintaining the vapors in said chambers the combined vapors expand and pass at high velocity at dilerent condition of pressure and temperature, said `from said next chamber into another chamber and so on, chambers being arranged in series according to an order each of said expansion nozzle means being in mutual of successively descending interior pressure and temalignment and increased in size from nozzle to nozzle. peratures, and expansion nozzle means interconnecting 2. Apparatus for condensing vapors comprising a yadjacent chambers in said series whereby vapors of higher plurality of chambers for containing vapors, means assopressure and temperature will expand and pass at high ciated with said chambers for maintaining the vapors in velocity from one chamber into the next and combine with said chambers at diierent conditions of pressure and the vapors in said next chamber and the combined vapors expand and pass at high velocity from said next chamber into another chamber and so on, said expansion nozzle means being closely positioned from chamber to chamber and aligned to direct the vapors from said one chamber at high velocity against the vapors in said next chamber thereby eecting a kinetic energy transfer to the vapors in said next chamber to cause said vapors in said next chamber to move at high velocity together with the vapors from said one chamber through the next adjacent nozzle means.

References Cited UNITED STATES PATENTS Hammond 202-173 Schmidt 62-270 Follain 62-27OX Kirgan 62-270 N011 202-173UX Bethon `62-174 Chirico 62-173 Langer et al. 62-173 Lockman 62-159 OTHER REFERENCES The Inst. of Mechanical Engineers-Flash Evaporators for the Distillation of Sea-Water, by Frankel, pp. 39.

l5 NORMAN YUDKOFF, Primary Examiner F. E. DRUMMOND, Assistant Examiner 4U.S. C1. X.R. 

